Apparatus and Method for Biogas Purification

ABSTRACT

The present invention is a biogas processing system having a compressor having a biogas input and output, a pump having a water input and output, a scrubber tower having a mixing chamber connected to a biogas input, a water pump input, a water output, and a processed biogas output, and a filtration member connected to the water output to remove contaminants from the water exiting the first scrubber tower. The system also includes devices for heating and cooling the recycled flow of water to enhance the ability of the water to absorb contaminants from the biogas and the ability of a stripper to remove absorbed contaminants from the water in a closed loop water system, and a controller for closely controlling the operating parameters of the system to achieve safe an optimal operation of the system.

FIELD OF THE INVENTION

The present invention relates to systems and methods for thepurification of biogas, and in particular to the production of highpurity natural gas from a biogas source for use as an energy source.

BACKGROUND OF THE INVENTION

Machines of all sorts rely upon refined petroleum products, such as gasand motor oil, in order to operate. The increasing number of machinesbuilt and sold each year ensures that the amount of fuel supplied in agiven period of time will eventually not be able to support all thevehicles in operation. Additionally, there are significant andwide-spread concerns about the environmental aspects of fossil fuelsattributed significantly to global warming. Fossil fuels are anon-renewable resource having only a finite supply which has sparkedconcern about energy shortages or a world-wide energy crisis if fossilfuel production ceased or otherwise lagged behind demand. Therefore,alternative energy and fuel research is an important and competitiveindustry.

Natural gas is one of the cleanest burning fossil fuels, and millions ofvehicles worldwide have been modified or built to run on it. In fact,the infrastructure to support the use of natural gas has been developedin some areas where its purer combustion properties are highly valued.Unfortunately, there are a number of drawbacks to using natural gas as atransportation fuel. First, natural gas is still a non-renewableresource. The finite supply of natural gas means the price fluctuateswith production. In general, natural gas is not an economicallycompetitive alternative for most consumers. Also, burning natural gasstill contributes to global warming gases. Finally, the energy densityat which combustion occurs is over one thousand times less thanconventional liquid fuels. In order to overcome its low energy density,natural gas must be highly pressurized. High pressures must be combinedwith low temperatures in order to convert natural gas into a dense,easily transported liquid fuel.

Natural gas mainly consists of methane (CH.sub.4), but, depending on theterrestrial origin of the gas, it can contain other trace gases such ashydrogen sulfide, hydrogen, propane, butane, etc. While natural gas is anon-renewable resource, methane is generated as a natural by-product ofanaerobic fermentation or digestion, which is a ubiquitous environmentalprocess essential for reducing organic matter in the naturalenvironment. The main by-products of anaerobic digestion are methane, atgenerally one-half to two-thirds of the resulting gas, and carbondioxide, along with trace levels of hydrogen sulfide, oxygen, nitrogenand water vapor. Almost all of the energy in the original biodegradableorganic matter is contained in this renewable source of methane.

One alternative to the heavy reliance on fossil fuels involves purifyingthe gas that results from anaerobic digestion, also known as “biogas,”in order to produce a pure, renewable methane stream. Typically,anaerobic digestion devices (i.e., anaerobic digestion that is notoccurring in nature) are intended to convert organic material, alsoknows as “biomass,” from one form to another. For example, biomass canbe placed in a silo for partial fermentation that converts the biomassto animal feed. Anaerobic digestion is also used to treat plant, animaland human waste. These waste materials can be converted into afertilizing material. Yet, methane produced from anaerobic digestionwould still need to be compressed to greater than 2000 pounds/inch.sup.2(2000 ‘psi’) in order to approach the energy density of conventionalliquid fuels. Even at 2000 psi, methane is a gas, and it would need tobe purified, for some applications, before being used as a fuel. Knownbiogas purification and compression methods and apparatuses can notproduce a cost-effective fuel. As such, methods and devices forproducing biogas from anaerobic digestion have been rejected as viablealternatives for the production of fuel. A suitable process wouldprovide a renewable fuel source while treating waste products that mustotherwise be disposed of as well as being capable or using most sourcesof photosynthetically fixed biomass.

The fuel in biogas powered machines uses the same engine configurationas natural gas machines. The gas quality demands are strict. The rawbiogas from a digester need to be upgraded in order to obtain biogaswhich: 1) has a higher calorific value in order to provide more energyoutput; 2) has a regular/constant gas quality to obtain safe operationof the machine utilizing the biogas as an energy source; 3) does notenhance corrosion due to high levels of hydrogen sulfide, ammonia, andwater; 4) does not contain mechanically damaging particles, 5) does notgive ice-clogging due to a high water content and 6) has a declared andassured quality. In practice, this means that carbon dioxide, hydrogensulfide, ammonia, particles and water (and other trace components) haveto be removed so that the product gas for vehicle fuel use has methanecontent above 95%. Different quality specifications for vehicle fuel useof biogas and natural gas are applied in different countries.

A number of biogas upgrading technologies have been developed for thetreatment of different sources of biogas, such as natural gas, sewagegas, landfill gas, etc. At present, four different methods are usedcommercially for removal of carbon dioxide from biogas either to reachvehicle fuel standard or to reach natural gas quality for injection tothe natural gas grid.

Primarily, water scrubbing is used to remove carbon dioxide but alsohydrogen sulfide from biogas, since these gases are more soluble inwater than methane. The absorption process is purely physical. Usuallythe biogas is pressurized and fed to the bottom of a packed column wherewater is fed to the top so the absorption process is operatedcounter-currently. The water which exits the column with absorbed carbondioxide and/or hydrogen sulfide can be regenerated and re-circulatedback to the absorption column. The regeneration is made bydepressurizing or stripping with air in a similar column. Stripping withair is not recommended when high levels of hydrogen sulfide are handledsince the water will soon be contaminated with elementary sulfur whichcauses operational problems. The most cost efficient method is not tore-circulate the water if cheap water can be used, for example, outletwater from a sewage treatment plant.

However, this purification process has a number of limitations, inparticular, the inability to significantly remove the O.sub.2 and/or theN.sub.2 components of the biogas. The O.sub.2 and N.sub.2 present in thebiogas can build up over time and negatively affect the purity of thenatural gas, making unsuitable for introduction directly into a naturalgas pipeline. In addition, the amount of water that is necessary toenable the stripping process to operate effectively is very high, whichmakes the utilization of suitable water-regeneration processesundesirable.

Therefore, there exists a need for a system for methane production usingbiogas produced as the result of anaerobic digestion or other similarprocesses that can sufficiently remove not only the primary contaminantsfrom the biogas, such as carbon dioxide and hydrogen sulfide, but alsomore trace impurities, e.g., O.sub.2, N.sub.2, and moisture to produce apipeline quality natural gas.

SUMMARY OF THE INVENTION

According to one object of the present invention, a biogas processingsystem includes a series of key functional elements which whensequentially combined and properly controlled will consistently purifyraw biogas to meet or exceed F.E.R.C. specifications for commercialpipeline quality natural gas. The biogas processing system includes ameans for removing water and/or hydrogen sulfide from biogas before thebiogas enters a first compressor having a biogas input and a compressedbiogas output, a first pump having a water input and a water output, anda first scrubber tower. The first scrubber tower includes a mixingchamber, a compressed gas input, a water input coupleable to the wateroutput of the first pump, a water output, and a processed gas output.The mixing chamber is in communication with the compressed gas input,the compressed gas output, the water input and the water output. Thebiogas processing system also includes a second scrubber tower having amixing chamber, a compressed gas input in communication with the outputof the first scrubber tower, a water input, a water output, and aprocessed gas output. The biogas processing system further includes aflash tank having a water input coupled to the water output of the firstscrubber, a water output, and a gas recirculation output. To removeunwanted oxygen from the process stream, the water used in the scrubbertower is passed through a recycling system that utilizes a flash tank,air degasification and a membrane filtration system to clean the waterprior to reintroduction of the water into the scrubbers. In addition,suitable anion/cation bed technology can be employed to further cleanthe water, thereby prevent build up of these impurities in the biogasstream.

According to another aspect of the present invention, the temperature ofthe water exiting the scrubber tower(s) is modified prior to enteringthe recycling system in order to enhance the ability of the recyclingsystem to remove those contaminants contained within the water exitingthe scrubbers. This temperature change is effected by passing the waterthrough a number of other components of the system to cool the processstreams flowing through those components prior to being directed intothe recycling system.

According to still another aspect of the present invention, the systemand method further includes remotely monitoring the processing ofbiogas, and sending a command from a remote location to adjust at leastone processing parameter and electrically executing the command. Theremote sensing and communication systems allow for remote monitoring andremote control of the processing system, which can be advantageousbecause staffing is not necessarily available at all times at remoteprocessing locations. In some examples, the system requires little or noon-site human supervision.

Numerous other aspects, features, and advantages of the presentinvention will be made apparent from the following detailed descriptiontaken together with the drawing FIGURE.

BRIEF DESCRIPTION OF THE DRAWING FIGURES

The drawing illustrates the best mode currently contemplated ofpracticing the present invention.

In the drawings:

The drawing FIGURE is a schematic illustration of a biogas purificationsystem constructed according to the present invention.

DETAILED DESCRIPTION OF THE INVENTION

The following detailed description includes references to theaccompanying drawing, which form a part of the detailed description. Thedrawing shows, by way of illustration, a specific embodiment in whichthe invention may be practiced. This embodiment, which is also referredto herein as an “example,” is described in enough detail to enable thoseskilled in the art to practice the invention. The embodiment may becombined, other embodiments may be utilized, or structural, logical andelectrical changes may be made without departing from the scope of thepresent invention. The following detailed description is, therefore, notto be taken in a limiting sense, and the scope of the present inventionis defined by the appended claims and their equivalents.

In this document, the terms “a” or “an” are used, as is common in patentdocuments, to include one or more than one. In this document, the term“or” is used to refer to a nonexclusive or, unless otherwise indicated.Furthermore, all publications, patents, and patent documents referred toin this document are incorporated by reference herein in their entirety,as though individually incorporated by reference.

The drawing FIGURE is a schematic illustration of an example of a biogasprocessing system 100 that includes a biogas compression system 300,biogas scrubber system 400, water supply system 500, and analysis andfinal processing system 600. Water and biogas are processed throughcomponents of the biogas compression system 300, biogas scrubber system400, water supply system 500, and analysis and final processing system600 to process biogas into a more usable form, such as methane. In thesystem 100, each of the various components of the subsystems 300, 400,500, 600 and 700 are connected by suitable members, such as piping, thatconduct the material handled by the particular subsystem 300, 400, 500,600 and 700 between the components of the subsystem 300, 400, 500, 600and 700 at the required temperatures and pressures for proper operationof the subsystem 300, 400, 500, 600 and 700 in a manner as is known inthe art.

In an exemplary embodiment, the system 100 includes one, and preferablymultiple digesters 200 or other suitable sources of raw biogas that issupplied to the system 100. In some embodiments of the invention, theraw biogas is produced at a biogas site utilizing anaerobic digestion oforganic materials, e.g., manure, e.g., human, hog, turkey, chickenand/or cattle manure. The organic materials may be located at a biogassite, e.g., a landfill or a farm. Raw biogas typically includes amixture of carbon dioxide and methane with trace levels of hydrogensulfide and water vapor, and more particularly containing 55%-75% ofmethane, 25%-40% carbon dioxide and other components, such as hydrogensulfide, oxygen and nitrogen gases. The biogas from the digesters 200 isalso saturated with water at a pressure of about 4-12 psig, with avolumetric flow range from the digesters 200 of approximately5,000-50,000 standard cubic feet per hour.

The raw biogas is then directed via suitable conducting member, such aspiping, to a biogas compression system 300, where the biogas is treatedto remove the hydrogen sulfide and water, and to compress the biogas forfurther processing by the system 100.

The biogas compression system 300 includes a hydrogen sulfide cleaningsystem 302, a moisture knockout vessel 307, a first compressor 308, anaccumulator 312, a pre-conditioner 314, a second compressor 316 and acooler 318 that are each connected to one another by suitable piping 309that also includes one or more valves 310 to control the flow of biogasbetween the components of the system 300.

Raw biogas is initially fed from the digesters 200 through the hydrogensulfide cleaning system 302, which removes hydrogen sulfide from thebiogas. Hydrogen sulfide is removed in the system 302 by any suitableprocess, such as by air/oxygen dosing to the digester biogas, and ironchloride dosing to the digester slurry, among others. However apreferred method for removal of at least a portion of the hydrogensulfide in the system 302 is to pass the biogas through an iron spongeunder proper conditions to oxidize the hydrogen sulfide. The reasons forthe removal of the hydrogen sulfide are because the presence of sulfurgases, i.e., hydrogen sulfide, downstream will aggressively degrademetal equipment and sensors, and hydrogen sulfide is also a personnelhazard, even when present at very minor concentrations, which requiresits removal from the biogas stream.

The biogas passes out of the hydrogen sulfide cleaning system 302 and isdirected into the moisture separator 307. The moisture separator 307reduces the moisture content of the biogas from the saturated moisturecontent present when exiting the digester 200 to less than about 1.4%.Any condensed moisture present downstream will create problems forsystem control as it interferes with gas flow and pressure measurements.If not removed, condensation also causes rapid failure of compressorlube oil filters and internal lubricated parts.

The biogas output from the moisture separator 307 enters the firstcompressor 308, which is powered by a motor (not shown) which can be anelectric motor powered by a generator that is powered by abiogas-operable engine or a crude methane-operable engine (not shown).Using biogas or methane energy to power the motors allows the system tobe self-contained.

After passing through the compressor 308, the biogas enters anaccumulator 312 that combines the compressed biogas stream with recycledgas streams coming from a flash tank 413 and gas drier 610. The combinedbiogas stream is then directed from the accumulator 312 into apre-conditioner 314. The pre-conditioner 314 serves to pre-cool acceptedbiogas to separate and remove condensed moisture.

From the pre-conditioner 314 the biogas stream is directed through thesecond compressor 316 and into the cooler 318. In the cooler 318 thebiogas stream is thermally contacted with a cooling water stream toreduce the temperature of the biogas stream below about 70° F. forintroduction into the scrubber system 400.

The compressed and cooled biogas is supplied to the biogas scrubbersystem 400. Biogas processing plants typically remove carbon dioxidefrom biogas through water absorption. Water absorption or “waterscrubbing” techniques are predicated on the relative solubility ofmethane and carbon dioxide in water. Carbon dioxide is more soluble inwater under pressure than at atmospheric pressure. Methane is mostlyinsoluble even at elevated pressures. Pressurizing a methane/carbondioxide biogas mixture in the presence of water drives carbon dioxideinto solution in the water but drives little methane into solution. Theresulting processed biogas has an enriched methane content because someor all of the carbon dioxide has been processed out of the gas and intosolution in the water. The optimum relative solubility difference formethane and carbon dioxide is in the range from one hundred fifty (150)to two hundred (200) pounds per square inch gauge (psig). The compressedoperating pressure is a function of the temperature, carbon dioxide molefraction in the gas, and the desired methane purity.

The scrubber system 400 is also connected to a water supply system 500that pumps water into the scrubber system. The gas flows in counter-flowor cross-flow with the water. As the gas flows past the water, carbondioxide is absorbed into the water. Some methane is typically alsoabsorbed into the water. However, substantially less methane is absorbedinto the water than carbon dioxide because of the difference in relativewater solubility between methane and carbon dioxide. In an example, atabout 200 psig, nearly all of the carbon dioxide in biogas is absorbedinto water and about 5% of methane is absorbed, even though methane isthe more prevalent component in biogas.

In the drawing, the biogas scrubbing system 400 includes first andsecond scrubber towers 411, 412 and a flash tank 413 each connected bysuitable piping 414 and a number of valves 416, though different numberof scrubbing towers can be employed as desired. Preferably, the scrubbertowers 411 and 412 move biogas and water in counter-flow. For example,the scrubber towers 411 and 412 can includes one or more internalvertical columns that contain Rashig rings, sieve plates, bubble cap ordisk and donut gas/liquid contact devices. In another embodiment, thescrubber system 400 includes one or more cross-flow chambers in whichwater is passed in cross-flow over the biogas. The compressed biogas isintroduced at or near the bottom 420 of tower 411. Water is introducedat or near the top 421 of the tower 411. As the water moves down thetower, biogas flows up the tower and exits near the top 421 of the tower411. At least some of the carbon dioxide in the gas is absorbed into thewater. The gas exiting the top of the tower 411 has a higherconcentration of methane than the gas entering the bottom of the tower411 because some of the carbon dioxide is removed from the gas. In thepreferred embodiment shown in the drawing FIGURE, two sequentialscrubber towers 411 and 412 are used. The gas exiting the top 421 of thefirst tower 411 is introduced into the bottom 422 of the second tower412. Water enters at the top 423 of the second tower 412 and gas isintroduced at the bottom 422 of the second tower 412. In the system 100shown in the drawing FIGURE, the biogas flows in counter-current to thewater, i.e., water exiting the bottom of the second tower enters a pump425 and is delivered to the top of the first tower 411. In analternative embodiment, water can be provided directly to each tower 411and 412 instead of circulating through the towers 411 and 412. Supplyingthe water in counter-current to the gas makes more efficient use of thewater. In addition, directly supplying fresh or de-gassed water providesmore efficient or effective biogas scrubbing in certain situations, forexample, when the water would become saturated with carbon dioxide incounter-current flow through the towers 411 and 412.

The carbon dioxide-laden water generated in the water scrubbing towers411 and 412 is passed to a flash vessel or tank 413 operated at a lowerpressure than the water scrubber towers 411 and 412 which pulls at leastsome of the methane out of the water. In particular, the water outputfrom the scrubber towers 411 and 412 is at about one hundred fifty (150)to about two hundred (200) psig, and the flash tank is at about 25-100psig. Because of the difference in solubility between methane and carbondioxide, methane desorbs out of the water more quickly and easily thancarbon dioxide. The reclaimed methane that is flashed out of the waterin the flash tank 413 is then introduced back into the biogas stream atthe accumulator 312.

The biogas stream that exits the scrubber system 400 through the top 423of the tower 412 is a purified, processed or “cleaned” biogas whichessentially comprises crude methane. This processed biogas issubsequently delivered to an analysis and final processing system 600.The analysis and final processing system 600 removes water vapor andtrace contaminants from the processed gas, tests the composition of thegas, and compresses the gas for storage or transport via truck orpipeline.

Initially, the processed biogas is passed through a drier and purifier610 that removes water vapor and trace contaminants remaining in theprocessed biogas. Air driers and purifiers are commercially available,for example, from Pioneer Air Systems. Driers and/or purifiers andrelated components are described in U.S. Pat. Nos. 4,761,968, 4,638,852,4,499,033, 5,107,919 and 5,207,895, among others.

Downstream from the drier and purifier 610, the analysis and finalprocessing system 600 includes gas analyzers 620 which sample theprocessed gas to determine its makeup. The parameters for the gasmeasured by the analyzers 620 can be calibrated to ensure the processedgas meets either FERC or DOT standards for compressed natural gas (CNG)or liquefied natural gas (LNG).

The parameters for each of these standards are shown in Table 1:

TABLE 1 Natural Gas Standards Component or Property Units of MeasureFERC Pipeline Spec CNG Spec per DOT Water vapor Lbs per mmscf Less than6 Less than 0.5 (million std cu ft) Hydrogen sulfide Grains per Ccf Lessthan or equal to Less than or equal to 0.25 0.10 Total sulfur Grains perCcf Less than or equal to Less than 0.1 20 Heating value Btu per CubicFoot Greater than or equal to 950 Temperature Degrees Fahrenheit Lessthan or equal to 120 F. Oxygen Percent by volume Less than or equal toLess than 1.0 0.2 Carbon dioxide Percent by volume Less than or equal toLess than 3.0 2.0 Non-hydrocarbon Percent by volume Less than 4.0 gases

If the analyzers 620 determine that the processed gas is outside of oneor more of these parameters, the analyzer 620 will cause the gas to bedirected via valves 630 to either local flare 1000 for combustion, or toa storage tank 625 and compressor 635 for subsequent direction to theaccumulator 312 for re-introduction into the scrubbing system 400 forfurther cleaning.

However, if the process gas has been sufficiently purified to meet thestandards set in the analyzers 620, the gas is directed by the valve 630to one or more tanks 640 or for use within the facility housing thesystem 100, or to mobile storage tanks 640′ used to transport the gas toanother location for use. For that portion of the processed gas directedto the storage tanks 640, the gas can be directed to third and fourthcompressors 650 and 660 driven by a suitable motor (not shown) that isoptionally coupled to a biogas or methane-operable combustion engine(not shown). In an example, the compressors 650 and 660 compress theprocessed gas to up to about 3600 psig to produce CNG or LNG which canthen be delivered to a tanker trailer (not shown) or to a pipelineconnection 670. The gas directed into the pipeline connection 670 canalso be taken from storage tanks of a companion module or system 680that is connected to the system 100 at a connection point 690, and thatoperates identically to the system 100 to produce the purified biogas.

The system 100 also includes a water supply system 500. The water supplysystem 500 includes a water reservoir 510 to which is attached a watermakeup valve 535 to provide a source of water to replenish the amount ofwater lost through the normal operation of the system 100. A water pump512 is disposed within the reservoir 510 and used to supply water to thepiping 514 connecting the various components of the system 500.Additionally, while the system 500 does utilize the water makeup valve535, the system 500 is designed as a closed loop system, therebymaximizing the utility of the water initially contained in the system500. Further, the components of system 500, when arranged in propersequence, afford maximum benefit of thermal exchanges utilizing thewater contained in the system 500 to apply needed cooling of thecompressors in system 300 and system 600 while providing beneficialheating of the water in the system 500 for optimum degasification, andfor aiding other key process separations. This also minimizes additionalenergy consumption for waste heat removal and/or heat input, making thesystem 100 more efficient.

In a preferred embodiment of the system 100, when operated, the pump 512initially drives water from the reservoir 510 into a heat exchangedevice 518 operably connected to a compressor cooling system 700. Thesystem 700 is operably connected to the third compressor 650 thatoperates to compress the purified biogas prior to injection into thepipeline connection 670. Fluid contained within the system 700 isdirected by a pump 702 through a chiller 704 to cool the fluid withinthe system 700. The cooled fluid then flows from the chiller 704 into aheat exchange device 706 that can be selectively operated through theuse of a valve 710 to thermally contact the hydraulic operating fluidfor the third compressor 650 with the cooled fluid from the chiller 704.When the valve 710 is opened, the hydraulic fluid passes through thedevice 706 to thermally contact, and be cooled by the cooled fluid fromthe chiller 704 to enable the third compressor 650 to be operated mosteffectively. From the device 706, the fluid passes through the heatexchange device 518 prior to re-entering the chiller 704 to thermallycontact the water from the reservoir 510. Thus, the fluid in the system700 also effectively provides a reduction in temperature for the waterin the system 500. This cooling of the water to maintain an inlettemperature below 70 F provides enhanced gas absorption properties forthe water within the scrubbing towers 411 and 412, consequentlyincreasing the amount of biogas contaminants removed from the biogas bythe water contacting the biogas in the towers 411 and 412.

From the device 518, the water is pressurized by a booster pump 525 andflows into one or more membrane separation devices 520 that effectivelyreduces the amount of certain components that have absorbed by thewater, such as any hydrogen sulfide, carbon dioxide, ammonia and inparticular, nitrogen and oxygen. These biogas components tend toaccumulate in the system 100 over time as the result of migration fromthe various devices that remove the components, thereby reducing thecapacity of the water to absorb the biogas components from raw biogas.Because the system 500 operates to re-circulate the water within thesystem 500 for continuous usage, thereby utilizing a minimum quantity ofwater for water conservation purposes, properly cleaning there-circulated water is imperative for making the system 500 a closedloop. Thus, the device 520 effectively removes these biogas componentsfrom the water to improve the absorption qualities of the water. In aparticularly preferred embodiment, the device 520 is a passive flowthrough micro fiber contactor, such as a Liqui-Cel® membrane contactorfrom Membrana of Charlotte, N.C., which, when vacuum is applied, offersthe benefit of simultaneous dissolved oxygenand nitrogen removal and allother necessary degassing with one step. It is necessary to filter anysediment from the water to five (5) micron levels before the waterenters the device 520 to protect its integrity. In another embodiment,multiple devices 520 are employed in conjunction with an automatedmultiplexed filtration system 560 that can filter the water through oneof multiple filtering devices 520 contained in the filtration system560. The filtration system 560 allows continuous use and maintenance ofthe filter devices 520 in the filtration system when pressure dropsincrease as a result of filter loading by its capacity to direct thewater flow via valves 535 through a previously unused filter device 520within the filtration system 560 while the previously used device 520 isserviced or replaced.

After exiting the device 520, the water in the system 500 is directed bya pump 522 into the scrubbing towers 411 and 412 to effectively absorband remove the carbon dioxide and other biogas contaminants from thenatural gas in the manner described previously for the scrubbing system400. When the water exits the second tower 411, the water is directedinto the flash tank 413 where the methane absorbed by the water isreclaimed, at least in part.

Upon exiting the flash tank 413, the water can optionally be directed byvalves 530 to the cooler 318 and/or a heat exchange device 532. Thewater directed to the cooler 318 thermally contacts the biogas streamfrom the pre-conditioner 314 and compressor 316 to effectively reducethe temperature of the biogas, while consequently increasing thetemperature of the water. Further, either after or without passingthrough the cooler 318, the water enters the heat exchange device 532that enables the water to thermally contact the hydraulic fluid used inoperating the compressor 316. Again, this thermal contact effectivelycools the hydraulic fluid, making the operation of the compressor 316more effective, while increasing the temperature of the water.

After passing through one, both or neither of the cooler 318 and theheat exchange device 532, the heated water then is directed into acarbon dioxide stripper 540. The increased temperature of the water at110-140 F entering he stripper 540 allows the absorbed gases in thewater to be more effectively removed by the stripper 540, resulting in acleaner recycled water flow. The water entering the stripper 540 iscontacted in a counter-current fashion with an air flow from air source545 that is pressurized by a compressor 555 prior to introduction intothe stripper 540. The air flow removes the carbon dioxide and othercontaminants from the water in a manner as is known in the art.

The water output from the stripper 540 is supplied to the reservoir 510,from which the water can be re-circulated through the scrubbing system400 to clean additional volumes of biogas. With this construction, thewater supply system 500 is self contained and operable with no externalsupply of water except for the small amounts of water introduced throughthe makeup valve 535 from a suitable water supply 570. A self-containedsystem 500 is advantageous, because it enables the gas processing systemto operate regardless of the on-site water situation. Additionally, thewater from the makeup water valve 535 is provided externally, but themajority of the water requirement for the water supply system 500 is metby re-circulated water.

In the system 500, the device 520 is specifically configured to removeoxygen and nitrogen from the water stream due to the increasedconcentrations of these contaminants that are present in the waterstream as a result of the water passing through the stripper 540. As thestripper 540 is operated to remove the carbon dioxide absorbed from thebiogas that is dissolved in the water, the operation of the stripper 540results in increased amounts of oxygen and nitrogen being dissolved inthe water exiting the stripper 540. The increase in the oxygen andnitrogen concentrations is due to the air flow directed through thestripper 540 to remove the carbon dioxide from the water. Essentially, aportion of the oxygen and nitrogen in the air replaces the dissolvedcarbon dioxide that is being removed from the water.

If left in the water, the elevated oxygen and nitrogen concentrationsresult in a reduction in the amount of carbon dioxide that can beabsorbed by the water due to the presence of the oxygen and nitrogen.This, in turn, reduces the effectiveness of the water in being able toclean the biogas passing counter to the water within the scrubbingtowers 411 and 412.

In addition, the elevated amounts of oxygen and nitrogen present in thewater stream can be transferred from the water into the biogas streamwithin the scrubbing towers 411 and 412. Thus, instead of removing theoxygen and nitrogen contaminants, along with the carbon dioxide andother components, from the biogas stream, the water effectively adds tothe amounts of these contaminants already present in the biogas. This,in turn results in processed biogas that has amount of oxygen andnitrogen present that exceed the specifications for compressed naturalgas and pipeline quality natural gas, requiring that the gas bereprocessed. As a result, in addition to the benefit of creating theclosed loop water supply system 500 to significantly reduce the waterconsumption of the overall system 100, the filtration members 520 alsosignificantly reduce the levels of certain contaminants in the processedgas produced by the system 100 by removing these contaminants from thewater in the system 500 prior to the water contacting the biogas.

In addition to the features of the system 100 discussed previously, oneother significant aspect of the system 100 is the use of an automaticoperating and monitoring system 800 to control the operation of thevarious components of the system 100. The system 800 includes a numberof sensors 802 positioned on the various devices and components of thesystem 100 and operable to determine the particular operating parametersof the system 100. Each of the sensors 802 is operably connected via asuitable connection, e.g., wireless or hard wired line, to a controller804 that receives the data from each of the sensors 802 for comparisonwith normal operational parameters stored within the controllerconcerning the operation of each portion of the system 100. Thecontroller 804 is also operably connected via a suitable connection,e.g., wireless or hard wired line, to each of the operating controls(not shown) for the various components of each of the subsystems 300,400, 500, 600, and 700, as well as to an exterior communication network,such as the Internet 806 or a telephone line, in order to communicatethe data received from the sensors 802 to a selected electronic device808, such as a computer, PDA, telephone, or the like, monitored by aperson supervising the operation of the system 100 from either a localor remote location. Thus, the system 100 can be operated and controlledby the system 800 in a manned or unmanned configuration.

Should one or more of the sensors 802 determine that there is a problemwith or an out-of-spec parameter for the operation of a part of thesystem 100, the controller 804 is also directly operably connected toeach of the components of the system 100 or their operating mechanism(s)(not shown) such that the controller 804 can act to alter the operationof the component, or to safely shut down the component and/or theoverall system 100. In this circumstance, the controller 804 will alsobe able to alter the designated supervisor of the problem, such that theproblem can be corrected and the system 100 returned to normal operationas soon as possible.

During normal operation of the system 100, the controller 804 isconfigured to be able to response to changes in the outflow conditionsof the processed gas from the scrubbing system 400. For example, becausethe output volume and pressure of the biogas from the digester 200 canvary during the day, the control system 800 will automatically adjustits operation to utilize the available biogas to maximize gas generatingefficiency while protecting the digesters 200 and the associated boiler.

For example, the controller 804 employs a non-linear ramp logic togradually increase system pressure based upon the number of digesters200 available on startup for the system 100, as well as anytime theoperating pressure of the system 100 is adjusted. This logic used in thecontroller 804 effects the demand rate made on the digesters 200 suchthat, based on digester pressure, the controller 804 can automaticallyadjust the operating set points for the system 100 to lower systemdemand during periods of low gas availability and raise system setpoints to take advantage of higher levels of gas availability.

In addition, the system 100 has many interdependent control loops (notshown) for each of the various sub-systems 300, 400, 500, 600 and 700which can experience significant instability or oscillations during flowrate disturbances in any one or more of these systems. To account forand deal with these disturbances, the controller 804 includes adaptivelogic which monitors the rate-of-change of process variables for eachsub-system 300, 400, 500, 600 and 700 and their deviation from apredetermined set point to effectively modify the response for eachsub-system 300, 400, 500, 600 and 700 to changing operating conditions.For example, in the water supply system 500, this logic can beimplemented for monitoring the water level in the reservoir 510 and tomonitor water pressure in the pipes connecting the various components ofthe water supply system 500. In a particularly preferred embodiment, thelogic applies a calculated rate of change multiplier which is applied tothe original IGain parameter that is determined during loop tuning forthe water system 500 when the actual process variable rate-of-changeexceeds the normal rate-of-change and the direction of change is awayfrom the setpoint. The calculated rate of change multiplier isinfluenced by the amount of deviation from setpoint and therate-of-change of the process variable: i.e. the greater the deviation,the greater the Maximum Rate-Of-Change Multiplier and the greater therate-of-change, the greater the percentage of the Maximum Rate-Of-ChangeMultiplier applied to the original IGain parameter._The logic employedby the controller 804 is also selective as to when the modified responsewill be applied and the amount of response required response for eachsub-system 300, 400, 500, 600 and 700.

Also, because the system 100 is configured to supply gas directly into apipeline 670, the system 100 can potentially suffer significant downtimeif there are many short term instances of off spec gas from the scrubbersystem 400 since the determination by the analyzer 620 in the finalprocessing system 600 to cut off injection into the pipeline 670 must bemade almost instantaneously to maintain the quality of the gas in thepipeline 670. As a result, the system 100 includes the accumulationtanks 640 to batch or mix, and store on spec gas prior to finalcompression and injection into the pipe line 670. The control logicutilized in the controller 840 employs a weighted averaging schemeduring the filling of each of these tanks 640 which providesconsiderable tolerance during short periods when out of spec gas isdetected by the gas analyzer 620. The mixing and storage of certainamounts of off spec gas with previously stored on spec gas in the tanks640 enables the controller 840 to maintain continuous operations in theupstream sub-systems 300, 400, etc., while additionally maintainingacceptable pipe line quality for the gas stored in the tanks 640.

Furthermore, the water supply system 500 pumps against a head pressureas high as two hundred (200) psig during regular operation of thesub-system 500. If the water supply system 500 is shutdown for anyreason, it can be extremely difficult to re-establish the water flowthrough the sub-system 500 as a result of this head pressure. To remedythis potential situation, the controller 840 is configured toincrementally reduce the head pressure in the water supply system 500.For example, when a restart of the water system 500 occurs and the pump512 fails to establish flow within the water system 500 in a predefinedamount of time, the water system 500 is shutdown and the flow of biogasis directed toward plant flare 1000 so as to lower the overall pressurein the system 100. The compressor 308 is also slowed to a minimum speedto help drop system pressure. When the system pressure drops 5 psig, asdetermine by one or more of the sensors 802, the controller 804 restartsand monitors the system 500 for flow establishment. If the flow is notestablished, this is sensed by the controller 804 and the entire processis repeated after another 5 psig drop in the overall system pressure.Once flow is established, the gas cleaning system 100 will return tonormal operation by recharging the absorption columns 411, 412 withfresh biogas. Preferably, this function of the controller 804 is totallyautomatic, and does not require any operator intervention.

Also, during startup of the system 100, the water supply system 500 isbrought online as soon as the available system pressure, e.g., a minimumsystem pressure of 50 psig and a minimum differential pressure acrossthe valve 535′ controlling the level of water in the reservoir 510 of 13psig. Because this occurs at pressures well below the normal operatingpoint for the water supply system 500, the large primary booster pump512 is capable of overwhelming the flow capacity of the system 500 atstart up, thus causing the water supply system 500 to have to shutdowndue over-filled portions of the water supply system 500 and/or thebiogas scrubbing system 400. The avoid this problem, the controller 804is configured to gradually increase the water flow rate set point forthe water supply system 500 as system pressure increased. Once thenormal flow rate set point is achieved, the controller 804 cancontinuously monitor the flow rate to change the flow rate toaccommodate varying pressure conditions in the water supply system 500.

The controller 804 also has the capability to record all of theoperational data generated by the sensors 802, such as the quality ofthe gas being determined by the gas analyzer 620, and the volume of thegas stored in the tanks 640 and/or diverted into the pipeline connection670. For example, the controller 804 can safely route any off spec gasfrom the system 400 to another acceptance path or to flare. Thecontroller 840 can also perform weighted composition averaging of eachquality criterion for all gas produced for stable production withinspecification, and if outflow gas is rejected by a receiving valve,disabled by a compressor fault, or the lack of a fresh receivingtrailer, the controller 804 can determine or handle a safe routing forthe gas or initiate a shutdown of the system 100, while recording andreporting all events that caused the shut down.

While the system 800 also includes fully operational controls andinformational instrumentation at the site of the system 100, the system800 also allows for the system to be completely started, operated andshutdown remotely. In addition, an emergency power backup system 900 isconnected to the system 800 to power the system 800 including thesensors 802 and the controller 804 to maintain supervisory control ofthe entire system 100 for safe shutdown when electrical power fails.

Various other embodiments of the present invention are contemplated asbeing within the scope of the following claims particularly pointing anddistinctly claiming the subject matter regarded as the invention.

1. A biogas processing system comprising: a) a first compressor having abiogas input and a compressed biogas output; b) a first pump having awater pump input and a water pump output; c) a first scrubber towerhaving a first mixing chamber, a first compressed gas input, a firstwater input connectable to the water pump output of the first pump, afirst water output, and a first processed gas output, the first mixingchamber in communication with the first compressed gas input, the firstprocessed gas output, the first water input and the first water output;and d) a water filtration member operably connected to the first wateroutput, the filtration member configured to remove contaminants from thewater exiting the first scrubber tower.
 2. The biogas processing systemof claim 1, wherein the water filtration member is formed as part of awater supply system, the water supply system including: a) a heatingdevice operably connected to and downstream of the first water output;b) a stripping device operably connected between the first water outputand the first pump; and c) a water reservoir connected between thestripping device and the first pump.
 3. The biogas processing system ofclaim 2 wherein the water supply system is a closed-loop water supplysystem.
 4. The biogas processing system of claim 2 wherein the heatingdevice is a heat exchanger configured to thermally contact operatingfluid from the first compressor with the first water output.
 5. Thebiogas processing system of claim 2 wherein the heating device is abiogas cooler operably connected to and upstream of the first compressedgas input, and configured to thermally contact the first compressed gasinput with the first water output.
 6. The biogas processing system ofclaim 2 wherein the water supply system further comprises a coolingdevice disposed between the reservoir and the water pump input, whereinthe cooling device is configured to thermally contact the water pumpinput with a separate cooling means.
 7. The biogas processing system ofclaim 1 further comprising a hydrogen sulfide removal device operablyconnected to the biogas input of the first compressor.
 8. The biogasprocessing system of claim 1 further comprising a moisture separatordevice operably connected to the biogas input of the first compressor.9. The biogas processing system of claim 1, further comprising a coolingdevice operably connected to and upstream of the first water input. 10.The biogas processing system of claim 9 further comprising a secondcompressor operably connected to and downstream of the first processedgas output, and a cooling system operably connected to the secondcompressor, wherein the cooling system functions as the cooling device.11. The biogas processing system on claim 1 wherein the water filtrationmember is configured to remove oxygen from the water entering the waterinput of the first scrubbing tower.
 12. The biogas processing system ofclaim 1 wherein the water filtration member is a membrane contactor. 13.The biogas processing system of claim 1 wherein the water filtrationmember is configured to remove nitrogen from the water entering thewater input of the first scrubbing tower.
 14. The biogas processingsystem of claim 1 further comprising: a) a second pump having a secondwater pump input and a second water pump output; and b) a secondscrubber tower having a second mixing chamber, second a compressed gasinput, a second water input connectable to the water pump output of thefirst pump, a second water output, and a second processed gas output,the mixing chamber in communication with the second compressed gasinput, the second processed gas output, the second water input and thesecond water output; wherein the second compressed gas input isconnected to the first processed gas output, and the second water outputis connected to the first water input, and wherein the second water pumpis connected between the second water output and the first water input.15. The biogas processing system of claim 1 further comprising acontroller operably connected to the first compressor, the first pump,the first scrubber tower, and the water filtration member, thecontroller configured to adjust the operating parameters of at least oneof the first compressor, the first pump, and the first scrubber tower inresponse to changes a biogas flow connected to the biogas input of thefirst compressor.
 16. The biogas processing system of claim 15 whereinthe controller is configured to adjust the operating parameters of thefirst pump in response to changes in a flow of water through the firstpump.
 17. The biogas processing system of claim 16 wherein the change inthe flow of water through the first pump occurs during start up of thebiogas processing system.
 18. The biogas processing system of claim 1further comprising: a) a gas analyzer operably connected to the firstprocessed gas output of the first scrubber tower; b) at least onestorage tank operably connected to the first processed gas output of thefirst scrubber tower downstream from the gas analyzer; and c) acontroller operably connected to the gas analyzer and the at least onestorage tank, the controller configured to control a flow of processedbiogas into the at least one storage tank.
 19. The biogas processingsystem of claim 18 wherein the controller is configured to mixappropriate amounts of processed biogas exceeding pipeline qualitystandards with appropriate amounts of processed biogas below pipelinequality standards in the at least one tank to achieve an overall mixtureof processed biogas in the at least one storage tank that exceedspipeline quality standards.
 20. A method of processing a biogas, themethod comprising: a) providing a biogas processing system comprising afirst compressor having a biogas input and a compressed biogas output, afirst pump having a water pump input and a water pump output, a firstscrubber tower having a mixing chamber, a compressed gas input, a waterinput connectable to the water pump output of the first pump, a wateroutput, and a processed gas output, the mixing chamber in communicationwith the compressed gas input, the processed gas output, the water inputand the water output, and a water filtration member operably connectedto the water output of the first scrubber tower, the filtration memberconfigured to remove contaminants from the water exiting the firstscrubber tower; b) directing a flow of water from the first pump throughthe filtration member to filter the flow of water; c) directing a flowof biogas from the first compressor into the compressed gas input of thefirst scrubbing tower; d) directing the flow of water from thefiltration device into the water input of the first scrubbing tower tocontact the flow of biogas; and e) directing the flow of water from thewater output of the first scrubbing tower to the first pump.
 21. Themethod of claim 20 wherein the biogas processing system furthercomprises a heating device operably connected to and downstream of thewater output of the first scrubbing tower, the method further comprisingthe step of directing the flow of water through the heating device priorto directing the flow of water from the water output of the firstscrubbing tower to the first pump.
 22. The method of claim 20 whereinthe biogas processing system further comprises a cooling device operablyconnected to and upstream of the water input of the first scrubbing

at least one storage tank operably connected to the first processed gasoutput of the first scrubber tower downstream from the gas analyzer; anda controller operably connected to the gas analyzer and the at least onestorage tank, the controller configured to control a flow of processedbiogas into the at least one storage tank, and wherein the methodfurther comprises the steps of: a) directing the first processed gasoutput of the first scrubber tower through the gas analyzer afterdirecting controlling a flow of processed biogas into the at least onestorage tank after directing a flow of biogas from the first compressorinto the compressed gas input of the first scrubbing tower; and b)directing at least a portion of the first processed gas output of thefirst scrubber tower into the at least one storage tank.
 29. The methodof claim 28 wherein the step of directing at least a portion of thefirst processed gas output of the first scrubber tower into the at leastone storage tank comprises mixing appropriate amounts of processedbiogas exceeding pipeline quality standards with appropriate amounts ofprocessed biogas below pipeline quality standards in the at least onetank to achieve an overall mixture of processed biogas in the at leastone storage tank that exceeds pipeline quality standards.